CA2738003C - Device for burning a fuel/oxidant mixture - Google Patents
Device for burning a fuel/oxidant mixture Download PDFInfo
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- CA2738003C CA2738003C CA2738003A CA2738003A CA2738003C CA 2738003 C CA2738003 C CA 2738003C CA 2738003 A CA2738003 A CA 2738003A CA 2738003 A CA2738003 A CA 2738003A CA 2738003 C CA2738003 C CA 2738003C
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN A CARRIER GAS OR AIR
- F23C99/00—Subject-matter not provided for in other groups of this subclass
- F23C99/006—Flameless combustion stabilised within a bed of porous heat-resistant material
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Abstract
Device for burning a fuel/oxidant mixture in a strongly exothermic reaction, said device consisting of a reactor (1) with a combustion chamber containing at least one first porous material and at least one second porous material in separate zones A (2) and C
(3), whereby the zones are designed in such a way that an exothermic reaction can only occur in zone B(3), and with one or more feed lines for the fuel and for the oxidant, whereby zone A (2) which consists of the first porous material is separated by a distance of 10 mm to 4000 mm, preferably 20 mm to 500 mm, equating to one zone B (4), from zone C (3) which consists of the second porous material and is located before zone C (3) in flow direction of the fuel/oxidant mixture.
(3), whereby the zones are designed in such a way that an exothermic reaction can only occur in zone B(3), and with one or more feed lines for the fuel and for the oxidant, whereby zone A (2) which consists of the first porous material is separated by a distance of 10 mm to 4000 mm, preferably 20 mm to 500 mm, equating to one zone B (4), from zone C (3) which consists of the second porous material and is located before zone C (3) in flow direction of the fuel/oxidant mixture.
Description
09.22.2008 Device for burning a fuel/oxidant mixture The invention relates to a device for burning a fuel/oxidant mixture in a strongly exothermic reaction, said device consisting of a reactor with a combustion chamber containing at least one first porous material and at least one second porous material in separate zones, whereby the zones are designed in such a way that an exothermic reaction can only occur in the second zone, and with one or more feed lines for the fuel and for the oxidant.
Documents DE 43 22 109 C2 and DE 199 39 951 C2 describe devices which are designed as so-called porous burners.
According to this the combustible gas mixture initially flows through one region which below is referred to as zone A and which has such small effective pore diameters which do not allow stationary flame spreading. In other words, the first porous zone is operationally similar to a flame arrester. The following actual combustion region ¨ which is referred to as zone C in the following description ¨ has however greater pore sizes which are large enough to permit a stationary burning. A critical Peelet number of PE>65 is cited in technical literature (for example Babkin et al, in "Combustion and Flame, Vol. 89, pages 182-190, 1991) as criterion for the spreading of flames in the interior of a porous matrix.
Materials such as for example aluminum oxide, zircon oxide, silicon carbide, etc. which ¨ in addition to high temperature resistance also possess sufficient corrosion resistance - can be used as porous combustion chamber filling in porous reactors for chemical industrial plants. To produce a porous combustion chamber, bulk material of temperature resistant ceramic balls, saddle packing or similar bodies are used, as are preferably used for example as random packing for thermal separation processes. Bulk materials are preferred because they allow easy clean-up of deposits - for example of salt residues which occur in hydrogen chloride synthesis ¨ originating from the combustion gases. According to DE 43 22 109 C
in porous burners too, zones of different pore structure or respectively pore size are arranged in order to produce hydrogen chloride zones. This is done by using filler bodies of different sizes for zones A and C. In addition structured packing and foams may be used in zones A and B.
According to document DE 199 39 951 C2 an additional support grate can preferably be arranged between the porous structures formed by filler bodies in the two zones and having different pore sizes. Said support grate preventing the discharge of smaller sized filler bodies from zone A into the inter-spaces of the larger filler bodies in zone C. In burners where gases do not exit vertically in upward direction another gas-permeable grate is arranged at the gas exit from zone C which closes the combustion chamber. As a result it is possible to arrange the reactor in any random position despite the loose bulk of filling bodies in the combustion chamber.
The porous reaction chamber is preferably encased by a corrosion resistant cooled wall which consists for example of artificial resin-impregnated graphite. Cooling can be effected through cooling water, air or by the combustion gases themselves. Between the cooled wall and the combustion chamber is then preferably located an insulating intermediate layer of high temperature resistant, corrosion resistant and thernially insulating materials, which prevent loss of heat and which ensure that the desired combustion chamber temperature prevails at each location in the combustion chamber. According to the document DE 199 39 951 C2 this heavy insulation peunits an almost adiabatic process control without any temperature influence on the combustion process as a result of the cooled wall. The adiabatic process control permits, for example simple scale-up of such chemical reactors since heat transport properties are irrelevant to the cooled walls and the entire process in flow direction can be regarded almost one-dimensional.
Documents DE 43 22 109 C2 and DE 199 39 951 C2 describe devices which are designed as so-called porous burners.
According to this the combustible gas mixture initially flows through one region which below is referred to as zone A and which has such small effective pore diameters which do not allow stationary flame spreading. In other words, the first porous zone is operationally similar to a flame arrester. The following actual combustion region ¨ which is referred to as zone C in the following description ¨ has however greater pore sizes which are large enough to permit a stationary burning. A critical Peelet number of PE>65 is cited in technical literature (for example Babkin et al, in "Combustion and Flame, Vol. 89, pages 182-190, 1991) as criterion for the spreading of flames in the interior of a porous matrix.
Materials such as for example aluminum oxide, zircon oxide, silicon carbide, etc. which ¨ in addition to high temperature resistance also possess sufficient corrosion resistance - can be used as porous combustion chamber filling in porous reactors for chemical industrial plants. To produce a porous combustion chamber, bulk material of temperature resistant ceramic balls, saddle packing or similar bodies are used, as are preferably used for example as random packing for thermal separation processes. Bulk materials are preferred because they allow easy clean-up of deposits - for example of salt residues which occur in hydrogen chloride synthesis ¨ originating from the combustion gases. According to DE 43 22 109 C
in porous burners too, zones of different pore structure or respectively pore size are arranged in order to produce hydrogen chloride zones. This is done by using filler bodies of different sizes for zones A and C. In addition structured packing and foams may be used in zones A and B.
According to document DE 199 39 951 C2 an additional support grate can preferably be arranged between the porous structures formed by filler bodies in the two zones and having different pore sizes. Said support grate preventing the discharge of smaller sized filler bodies from zone A into the inter-spaces of the larger filler bodies in zone C. In burners where gases do not exit vertically in upward direction another gas-permeable grate is arranged at the gas exit from zone C which closes the combustion chamber. As a result it is possible to arrange the reactor in any random position despite the loose bulk of filling bodies in the combustion chamber.
The porous reaction chamber is preferably encased by a corrosion resistant cooled wall which consists for example of artificial resin-impregnated graphite. Cooling can be effected through cooling water, air or by the combustion gases themselves. Between the cooled wall and the combustion chamber is then preferably located an insulating intermediate layer of high temperature resistant, corrosion resistant and thernially insulating materials, which prevent loss of heat and which ensure that the desired combustion chamber temperature prevails at each location in the combustion chamber. According to the document DE 199 39 951 C2 this heavy insulation peunits an almost adiabatic process control without any temperature influence on the combustion process as a result of the cooled wall. The adiabatic process control permits, for example simple scale-up of such chemical reactors since heat transport properties are irrelevant to the cooled walls and the entire process in flow direction can be regarded almost one-dimensional.
In a porous reactor the reaction is conducted inside a porous matrix consisting of temperature resistant material. In deviating from conventional reactor devices it is not necessary to arrange the reactor in a voluminous combustion chamber or to locate such downstream.
From the reactor itself the hot reaction products flow without direct flame foimation. In DE 43 22 109 C2 it is suggested to use a clearly lower Peclet number for the first zone, and a clearly higher Peclet number for the combustion zone than the critical Peclet number of Pe = 65.
When the porous reactor is being ignited the combustion stabilizes at the interface between the two zones. Due to the smaller pore dimensions in the first zone no combustion occurs in this region in a stationary state, only pre-heating of the gas mixture. This characteristic also fulfills the most stringent safety regulations in regard to the danger of flashback in chemical plants.
Due to the excellent heat transfer between gas and solids phase inside the porous matrix these are in approximate theimal balance. The approximate thermal balance between gas and solids phase and the intensive blending inside the pore body essentially causes the disappearance of free flames in the combustion zone which is equipped with larger pores. The burning process is now perfoimed in an extended reaction area which can be classified as a combustion reactor, rather than combustion chamber with free flames.
According to document DE 199 39 951 C2 the pre-mixing chamber is part of and a safety relevant component of the described device.
A disadvantage of the existing construction folms exists in the locally restricted temperature acquisition by means of thermo-elements in the reaction zone. A further disadvantage of porous reactors whose porous layers are made up of bulk material consists in that the bulk material bodies are carried along by the gas flow in the case of a higher or suddenly increased gas throughput, thereby leading to changes in the bulk material density as well as in the Peclet number. A stable process control under greatly changing gas throughput conditions, especially for controlled burning of larger volumes of halogenated gases during abnormal occurrences is possible only to a very limited extent.
Some embodiments of the current invention may provide a reactor which permits the exothermic chemical reactions described above by reducing the above described disadvantages.
Some embodiments of the current invention may provide for a strong exothermic reaction based on the device for burning a fuel/oxidant mixture mentioned at the beginning; said device consisting of a reactor with a combustion chamber containing at least one first porous material and at least one second porous material in separate zones, whereby the zones are designed in such a way that an exothermic reaction can only occur in the second zone, and with one or more feed lines for the fuel and for the oxidant, whereby zone A
which consists of the first porous material is separated by a distance of 10 mm to 4000 mm, preferably 20 mm to 500 mm, equating to one zone B, from zone C which consists of the second porous material and is located before zone C in flow direction of the fuel/oxidant mixture.
According to one embodiment of the current invention, there is provided device for burning a fuel/oxidant mixture in an exothermic reaction, said device comprising a reactor with a combustion chamber containing at least one first porous material and at least one second porous material in separate zones, whereby the zones comprise means which enable the exothermic reaction to only occur in the second zone, and with one or more feed lines for the fuel and for the oxidant, wherein zone A which consists of the first porous material is located at a distance of 10 mm to 4000 mm, equating to one zone B, from zone C which consists of the second porous material and is located vertically before zone C in flow direction of the fuel/oxidant mixture, wherein zone A is located above zone B and C and wherein a support grate is provided at an interface area.
A preferred further development of the device provides that the combustion chamber and the porous materials consist of materials which are resistant to temperatures from 1000 C to 2400 C.
From the reactor itself the hot reaction products flow without direct flame foimation. In DE 43 22 109 C2 it is suggested to use a clearly lower Peclet number for the first zone, and a clearly higher Peclet number for the combustion zone than the critical Peclet number of Pe = 65.
When the porous reactor is being ignited the combustion stabilizes at the interface between the two zones. Due to the smaller pore dimensions in the first zone no combustion occurs in this region in a stationary state, only pre-heating of the gas mixture. This characteristic also fulfills the most stringent safety regulations in regard to the danger of flashback in chemical plants.
Due to the excellent heat transfer between gas and solids phase inside the porous matrix these are in approximate theimal balance. The approximate thermal balance between gas and solids phase and the intensive blending inside the pore body essentially causes the disappearance of free flames in the combustion zone which is equipped with larger pores. The burning process is now perfoimed in an extended reaction area which can be classified as a combustion reactor, rather than combustion chamber with free flames.
According to document DE 199 39 951 C2 the pre-mixing chamber is part of and a safety relevant component of the described device.
A disadvantage of the existing construction folms exists in the locally restricted temperature acquisition by means of thermo-elements in the reaction zone. A further disadvantage of porous reactors whose porous layers are made up of bulk material consists in that the bulk material bodies are carried along by the gas flow in the case of a higher or suddenly increased gas throughput, thereby leading to changes in the bulk material density as well as in the Peclet number. A stable process control under greatly changing gas throughput conditions, especially for controlled burning of larger volumes of halogenated gases during abnormal occurrences is possible only to a very limited extent.
Some embodiments of the current invention may provide a reactor which permits the exothermic chemical reactions described above by reducing the above described disadvantages.
Some embodiments of the current invention may provide for a strong exothermic reaction based on the device for burning a fuel/oxidant mixture mentioned at the beginning; said device consisting of a reactor with a combustion chamber containing at least one first porous material and at least one second porous material in separate zones, whereby the zones are designed in such a way that an exothermic reaction can only occur in the second zone, and with one or more feed lines for the fuel and for the oxidant, whereby zone A
which consists of the first porous material is separated by a distance of 10 mm to 4000 mm, preferably 20 mm to 500 mm, equating to one zone B, from zone C which consists of the second porous material and is located before zone C in flow direction of the fuel/oxidant mixture.
According to one embodiment of the current invention, there is provided device for burning a fuel/oxidant mixture in an exothermic reaction, said device comprising a reactor with a combustion chamber containing at least one first porous material and at least one second porous material in separate zones, whereby the zones comprise means which enable the exothermic reaction to only occur in the second zone, and with one or more feed lines for the fuel and for the oxidant, wherein zone A which consists of the first porous material is located at a distance of 10 mm to 4000 mm, equating to one zone B, from zone C which consists of the second porous material and is located vertically before zone C in flow direction of the fuel/oxidant mixture, wherein zone A is located above zone B and C and wherein a support grate is provided at an interface area.
A preferred further development of the device provides that the combustion chamber and the porous materials consist of materials which are resistant to temperatures from 1000 C to 2400 C.
A temperature monitoring device and an ignition device are advantageously arranged in zone B. The temperature monitoring device is preferably an infrared sensor which captures a range of 2 to 200 cm2 at the interface with zone C. An acquisition beyond the cited range is not possible according to the current state of the art.
5a A preferred further development of the device provides that it is arranged vertically and that zone A is located above zones B and C. The bulk material of zones A and C are arranged on support grates. Loosening or swirling up of the bulk material and a change in the flow resistance and thereby the Peclet-number is prevented by the dead weight of the bulk material bodies and the support grates. In addition, loosening of the bulk layer is in principle avoided by locating zone A
above zone C since, because of this, the bulk material C is pressed against the support grate in direction of gravitation.
According to another further development of the invention the method provides that the fuel/oxidant mixture and the additionally supplied gas are blended at least partially in a premixing device which is located upstream from the reactor. A relevant device according to this further development consists in that it comprises a pre-mixing chamber for the fuel/oxidant mixture from where this fuel/oxidant mixture flows into the combustion chamber.
The pre-mixing chamber located here in accordance with the further development enables a substantially better blending and a more effective conversion of the reactants which, for examples allows a reduction of the required methane component during the hydrogen chloride synthesis.
An advantageous further development of the invention provides in particular that the premixing chamber is designed so that the component of the mixture's flow speed in the premixing chamber in relation to the direction of the combustion chamber is greater than the flame speed in the combustion chamber.
The premixing chamber is thereby dimensioned so that a flame which may possibly occur in the premixing chamber is blown out in the event of an unintentional ignition in the entire operating area, for example during start-up.
5a A preferred further development of the device provides that it is arranged vertically and that zone A is located above zones B and C. The bulk material of zones A and C are arranged on support grates. Loosening or swirling up of the bulk material and a change in the flow resistance and thereby the Peclet-number is prevented by the dead weight of the bulk material bodies and the support grates. In addition, loosening of the bulk layer is in principle avoided by locating zone A
above zone C since, because of this, the bulk material C is pressed against the support grate in direction of gravitation.
According to another further development of the invention the method provides that the fuel/oxidant mixture and the additionally supplied gas are blended at least partially in a premixing device which is located upstream from the reactor. A relevant device according to this further development consists in that it comprises a pre-mixing chamber for the fuel/oxidant mixture from where this fuel/oxidant mixture flows into the combustion chamber.
The pre-mixing chamber located here in accordance with the further development enables a substantially better blending and a more effective conversion of the reactants which, for examples allows a reduction of the required methane component during the hydrogen chloride synthesis.
An advantageous further development of the invention provides in particular that the premixing chamber is designed so that the component of the mixture's flow speed in the premixing chamber in relation to the direction of the combustion chamber is greater than the flame speed in the combustion chamber.
The premixing chamber is thereby dimensioned so that a flame which may possibly occur in the premixing chamber is blown out in the event of an unintentional ignition in the entire operating area, for example during start-up.
An additional improvement in this connection is achieved in a further development of the invention by means of cooling in the premixing chamber.
Another advantageous further development provides that a porous material with interconnected cavities, sufficient and large enough for flame development is provided in the combustion chamber.
In particular, the porosity of the porous material with interconnected cavities changes in direction of the flame development into larger pores, whereby a critical Peclet number results for the size of pores at one interior contact surface, above which the flame development occurs and below which it is suppressed.
Combustion stabilization is achieved through the increase in the size of pores in flow direction, whereby a critical Peclet number for the size of pores results in one zone of the porous material, above which the flame development occurs and below which it is suppressed.
Application of this technology for the production of chemical products, such as for example hydrogen chloride, or for the afterburning of pollution gases, for example halogenated gases not only affects the combustion positively but also allows the line components in which the pore reactor is integrated to be designed and arranged advantageously.
The premixing chamber is constructed preferably of corrosion resistant materials, for example of artificial resin-impregnated graphite. Enamel or fluor carbon resin lined steel components can also be used to build a mixing chamber. From the premixing chamber the premixed gases penetrate preferably through a grate of corrosion resistant material, for example silicon-carbide, aluminum-oxide, or others, into zone A of the porous reactor. As previously discussed several chemical reactants such as chlorine and methane are suitable under the influence of UV-radiation for self-ignition. However, self-ignition in the premixing chamber should be avoided for safety reasons. A grate and the layout of zone A are selected so that no or very little UV-radiation reaches from zone A or respectively C into the premixing chamber which could cause ignition of the gas mixture of chlorine and methane.
The stability of the combustion in the described porous reactor is to be especially emphasized.
In contrast to the hydrogen chloride reactors which are constructed according to the current state of the art and which react very sensitively to pressure and volume fluctuations of the gases, whereby therefore the flame can easily extinguish, the combustion reaction in the porous reactor is immediately reignited through the heat capacity of the filler bodies in zone C, even during a short-tenn interruption of the gases. However, for safety reasons it is advisable to turn off the other gas during an outage of one of the gases, and to connect an inert gas flushing. Even after several minutes the reactor can then be operated again, without renewed start-up procedure, even after an inert gas flushing.
Ignition and preheating of the reactor can occur with a fuel gas (hydrogen, methane, or others) and air. Certainly, a conventional ignition device which is customary for such chemical reactors can be used. After completely heating zone C changeover to the reactants, for example chlorine, methane and air can occur gradually or immediately.
Sudden load fluctuations up to 50% of the rated load which can occur in this type of equipment can be controlled without difficulty in the described pore reactors.
Due to the technology for dimensioning of pore reactors, scaling-up for technical lines, especially with the previously described adiabatic process control according to which defined flow conditions are adhered to in zones A and C, independent of the equipment size, becomes surprisingly simple.
Another advantageous further development provides that a porous material with interconnected cavities, sufficient and large enough for flame development is provided in the combustion chamber.
In particular, the porosity of the porous material with interconnected cavities changes in direction of the flame development into larger pores, whereby a critical Peclet number results for the size of pores at one interior contact surface, above which the flame development occurs and below which it is suppressed.
Combustion stabilization is achieved through the increase in the size of pores in flow direction, whereby a critical Peclet number for the size of pores results in one zone of the porous material, above which the flame development occurs and below which it is suppressed.
Application of this technology for the production of chemical products, such as for example hydrogen chloride, or for the afterburning of pollution gases, for example halogenated gases not only affects the combustion positively but also allows the line components in which the pore reactor is integrated to be designed and arranged advantageously.
The premixing chamber is constructed preferably of corrosion resistant materials, for example of artificial resin-impregnated graphite. Enamel or fluor carbon resin lined steel components can also be used to build a mixing chamber. From the premixing chamber the premixed gases penetrate preferably through a grate of corrosion resistant material, for example silicon-carbide, aluminum-oxide, or others, into zone A of the porous reactor. As previously discussed several chemical reactants such as chlorine and methane are suitable under the influence of UV-radiation for self-ignition. However, self-ignition in the premixing chamber should be avoided for safety reasons. A grate and the layout of zone A are selected so that no or very little UV-radiation reaches from zone A or respectively C into the premixing chamber which could cause ignition of the gas mixture of chlorine and methane.
The stability of the combustion in the described porous reactor is to be especially emphasized.
In contrast to the hydrogen chloride reactors which are constructed according to the current state of the art and which react very sensitively to pressure and volume fluctuations of the gases, whereby therefore the flame can easily extinguish, the combustion reaction in the porous reactor is immediately reignited through the heat capacity of the filler bodies in zone C, even during a short-tenn interruption of the gases. However, for safety reasons it is advisable to turn off the other gas during an outage of one of the gases, and to connect an inert gas flushing. Even after several minutes the reactor can then be operated again, without renewed start-up procedure, even after an inert gas flushing.
Ignition and preheating of the reactor can occur with a fuel gas (hydrogen, methane, or others) and air. Certainly, a conventional ignition device which is customary for such chemical reactors can be used. After completely heating zone C changeover to the reactants, for example chlorine, methane and air can occur gradually or immediately.
Sudden load fluctuations up to 50% of the rated load which can occur in this type of equipment can be controlled without difficulty in the described pore reactors.
Due to the technology for dimensioning of pore reactors, scaling-up for technical lines, especially with the previously described adiabatic process control according to which defined flow conditions are adhered to in zones A and C, independent of the equipment size, becomes surprisingly simple.
The porous reactors which are described below, and are modified for chemical processes are parts of process technological equipment for the production of hydrochloric acid or for after-burning of halogenated, preferably chloride containing compounds.
Equipment of this type includes for example a modified porous reactor, a heat exchanger for cooling of the reaction products, or respectively for utilization of their heat content and, depending on the type of equipment includes also an absorber, scrubber or waste gas scrubber at transition pieces between the units, pumps, pipe lines and the usual safety, measuring and control devices. Because of the reaction control and the efficient blending of the gases in the porous reactor a voluminous combustion chamber is not necessary in contrast to the current state of the art. The reactor can be directly connected to the downstream equipment, for example to a heat exchanger, a quencher with absorber or other equipment. After the reaction products flowing from the reactor have been cooled in a heat exchanger or after a quencher, a partial flow of the cooled gases or gas mixtures are again supplied to the reactor, as previously described.
Alternatively, as described, another gas, for example water vapor can be added.
Depending upon the requirements for the product, only parts of the process technological equipment may be required, for example the reactor and gas cooler or reactor and quencher, depending upon whether the product is required in a gaseous faun or dissolved in water as hydrochloric acid.
An additional design foun of a line for the production of hydrogen chloride uses carbureted hydrogen gases as a hydrogen supplier, for example natural gas, methane, propane, etc., chlorine and air. Combustion occurs according to the greatly simplified illustration of the reaction equations (1) and (2):
CH4 + 02 + C12 -> CO + 2HC1 + H20 (1), CO + 1/202 -> CO2 (2).
Equipment of this type includes for example a modified porous reactor, a heat exchanger for cooling of the reaction products, or respectively for utilization of their heat content and, depending on the type of equipment includes also an absorber, scrubber or waste gas scrubber at transition pieces between the units, pumps, pipe lines and the usual safety, measuring and control devices. Because of the reaction control and the efficient blending of the gases in the porous reactor a voluminous combustion chamber is not necessary in contrast to the current state of the art. The reactor can be directly connected to the downstream equipment, for example to a heat exchanger, a quencher with absorber or other equipment. After the reaction products flowing from the reactor have been cooled in a heat exchanger or after a quencher, a partial flow of the cooled gases or gas mixtures are again supplied to the reactor, as previously described.
Alternatively, as described, another gas, for example water vapor can be added.
Depending upon the requirements for the product, only parts of the process technological equipment may be required, for example the reactor and gas cooler or reactor and quencher, depending upon whether the product is required in a gaseous faun or dissolved in water as hydrochloric acid.
An additional design foun of a line for the production of hydrogen chloride uses carbureted hydrogen gases as a hydrogen supplier, for example natural gas, methane, propane, etc., chlorine and air. Combustion occurs according to the greatly simplified illustration of the reaction equations (1) and (2):
CH4 + 02 + C12 -> CO + 2HC1 + H20 (1), CO + 1/202 -> CO2 (2).
This burning is difficult to control in lines according to the current state of the art since with unfavorable marginal conditions soot can occur, thus contaminating the equipment line and the acid. The descried special properties of the porous reactor unexpectedly pennit a stable, soot-free burning, also for this critical application.
As will be shown later with reference to design examples, porous reactors for after-burning of halogenated waste gases or vaporizable or gaseous, halogenated compounds are designed so that oxidants and fuel gas are preferably blown into the premixing chamber in a premixed state. In zone C, a stable support flame is produced by the high reaction enthalpy of oxidant and fuel gas.
The gas or gas mixture that is to be subject to after-burning is blown into the premixing chamber through a supply pipe, preferably over a support grate before zone A of the porous reactor, and mixed with the fuel/oxidant mixture. For temperature control of the after-burning process an appropriate surplus of the oxidant, especially air, is preferably used. To control the temperature in zone C of the porous reactor, the temperature is measured for example by means of an infrared pyrometer, and the signal being processed for the purpose of oxidant control.
The following devices differ during after-burning from the line components described above, depending on the halogen content of the waste gases. At a low halogen content where the fabrication of hydrochloric acid is not in the foreground only a quencher and a washer are generally located downstream. Other escort substances, for example sulfur compounds or similar, can also be subjected to a haimless removal in the described devices. In principle this applies also for halogenated or sulfurous vaporizable pure substances or mixtures. Since the described after burner equipment lines with porous reactor do not require a combustion chamber in the conventional sense, lines of this type can be arranged very compact and cost effective.
Based on the detailed descriptions outlined above, the following preferred further developments of the invention result in particular:
¨ the combustion chamber has at least two zones with material of different pore size, between which the pore size provides the critical Peelet number;
¨ the material with the interconnected cavities has at least partially a bulk deposit of bodies, such as are utilized for solid bodies bulk materials or controlled packing during thennal separation processes, such as balls or saddle packing;
¨ at the interface for zones of different porosity a grate, like a support grate is provided in order to prevent discharge of the bodies from one zone into the other zone, whereby the grate, especially the support grate can also be cooled;
¨ the combustion chamber is designed form flame stability during overpressure and negative pressure;
¨ all, or only some of the supplied product gases are preheated, in order to avoid condensing in the premixing chamber after adding cooling vapors, for example water vapor (condensed components would greatly deteriorate the reaction success and would lead to undesirable by-products);
¨ the premixing chamber is not being cooled, but its walls are targeted to be kept above the temperature of the dew point of the gas mixture, in order to prevent condensing of gas components.
The combustion chamber can now also be designed for flame stability during overpressure and negative pressure which, in the known state of the art, would have resulted only in insufficient flame stability. On the basis of the invention and its further developments however, a substantially greater pressure range is available, so that an appropriate design for a large pressure range in a manner known to the expert, in particular also for overpressure or negative pressure, can lead to a substantial increase in flame stability. Control systems can to a large extent be eliminated.
I
One preferred further development of the invention in particular provides a combustion chamber insulation for an approximate adiabatic burning control without wall effects.
An adiabatic combustion process is especially advantageous in increasing the conversion rate.
In addition to the burning it is also possible to gain reaction products, for example during hydrogen chloride burning for the hydrogen chloride synthesis. Here, a preferred further development of the invention provides that the apparatus includes a device for the extraction or separation of reaction products from the burned fuel/oxidant. Especially for the hydrogen chloride synthesis it is provided that the device is designed for a chlorinated compound in the fuel, as well as methane in the oxidant in order to burn the hydrogen chloride and includes a process technological unit after the combustion chamber for extraction of hydrogen chloride or hydrochloric acid. The described arrangement is known to the expert. It is to be remarked, in particular, that the appropriate safety devices are considered and that the materials are accordingly corrosion resistant.
As already discussed, the invention is not only suitable for burning and for hydrogen chloride synthesis, but also as a device for after-burning of waste gases and in this context especially for cleaning. Therefore, problem-free after-burning of components of chlorinated, organic compounds and thereby harmless disposal thereof is possible in some of design examples described below.
Additional measures and characteristic features in the invention result from the following description of one design example, with reference to the enclosed drawing:
Fig. I Partial illustration of a porous reactor line Porous reactor 1 which was previously discussed in more detail was selected for the following design example with which the invention can be implemented and which, in contrast to other reactor types offers special advantages. The essential characteristic of the invention consists in that the flame is cooled through addition of an additional gas to the fuel/oxidant mixture which can be realized in all conceivable reactor types. Therefore, the following description of the design example merely on the bases of porous reactor 1 is not to be regarded as a limitation.
One design foim of an inventive porous reactor 1 is illustrated in Fig. 1. The housing of porous reactor 1 consists of a thin-walled high temperature resistant ceramic interior lining 8, specifically oxide ceramic with a thickness of 2 mm to 50 mm, a graphite support casing 9 and an outside steel casing 10 located at a distance from it. Between the graphite support casing 9 and steel casing 10 cooling water is guided which leaves porous reactor 1 at connection piece 12.
In addition defined zones A ¨ 2, zone B ¨ 4 and zone C ¨ 3 are shown. Zone C ¨
3 is the zone in which burning occurs. Ignition is avoided in zone A -2 by means of appropriate dimensioning.
Zone C- 3 is filled with fillers for this purpose. Zone A -2 in contrast is filled with porous bodies which function as flame arrester. Zone A ¨ 2 and zone c ¨ 3 are distanced from each other by zone B ¨ 4. The wide-coverage temperature monitoring occurs at the interface between zone B ¨
4 and zone C ¨ 3 by means of access of a temperature sensor in the thermometer connecting piece. The gas mixture is led into porous reactor lfrom above, through premixing chamber 5.
The conversion of the reaction mixture occurs in zone C ¨ 3 which is located on support grate 7 and which, in addition is cooled by heat exchanger 11 which is located below it. The wall temperature in reaction zone C ¨ 3 is monitored by wall temperature sensor 13.
Component identification 1 Porous reactor 2 Zone A
3 Zone C
4 Zone B
Premixing chamber 6 Connection piece for temperature sensor 7 Support grate 8 Ceramic interior lining 9 Graphite walls Steel outside walls 11 Heat exchanger 12 Cooling medium connection 13 Wall temperature sensor ILl
As will be shown later with reference to design examples, porous reactors for after-burning of halogenated waste gases or vaporizable or gaseous, halogenated compounds are designed so that oxidants and fuel gas are preferably blown into the premixing chamber in a premixed state. In zone C, a stable support flame is produced by the high reaction enthalpy of oxidant and fuel gas.
The gas or gas mixture that is to be subject to after-burning is blown into the premixing chamber through a supply pipe, preferably over a support grate before zone A of the porous reactor, and mixed with the fuel/oxidant mixture. For temperature control of the after-burning process an appropriate surplus of the oxidant, especially air, is preferably used. To control the temperature in zone C of the porous reactor, the temperature is measured for example by means of an infrared pyrometer, and the signal being processed for the purpose of oxidant control.
The following devices differ during after-burning from the line components described above, depending on the halogen content of the waste gases. At a low halogen content where the fabrication of hydrochloric acid is not in the foreground only a quencher and a washer are generally located downstream. Other escort substances, for example sulfur compounds or similar, can also be subjected to a haimless removal in the described devices. In principle this applies also for halogenated or sulfurous vaporizable pure substances or mixtures. Since the described after burner equipment lines with porous reactor do not require a combustion chamber in the conventional sense, lines of this type can be arranged very compact and cost effective.
Based on the detailed descriptions outlined above, the following preferred further developments of the invention result in particular:
¨ the combustion chamber has at least two zones with material of different pore size, between which the pore size provides the critical Peelet number;
¨ the material with the interconnected cavities has at least partially a bulk deposit of bodies, such as are utilized for solid bodies bulk materials or controlled packing during thennal separation processes, such as balls or saddle packing;
¨ at the interface for zones of different porosity a grate, like a support grate is provided in order to prevent discharge of the bodies from one zone into the other zone, whereby the grate, especially the support grate can also be cooled;
¨ the combustion chamber is designed form flame stability during overpressure and negative pressure;
¨ all, or only some of the supplied product gases are preheated, in order to avoid condensing in the premixing chamber after adding cooling vapors, for example water vapor (condensed components would greatly deteriorate the reaction success and would lead to undesirable by-products);
¨ the premixing chamber is not being cooled, but its walls are targeted to be kept above the temperature of the dew point of the gas mixture, in order to prevent condensing of gas components.
The combustion chamber can now also be designed for flame stability during overpressure and negative pressure which, in the known state of the art, would have resulted only in insufficient flame stability. On the basis of the invention and its further developments however, a substantially greater pressure range is available, so that an appropriate design for a large pressure range in a manner known to the expert, in particular also for overpressure or negative pressure, can lead to a substantial increase in flame stability. Control systems can to a large extent be eliminated.
I
One preferred further development of the invention in particular provides a combustion chamber insulation for an approximate adiabatic burning control without wall effects.
An adiabatic combustion process is especially advantageous in increasing the conversion rate.
In addition to the burning it is also possible to gain reaction products, for example during hydrogen chloride burning for the hydrogen chloride synthesis. Here, a preferred further development of the invention provides that the apparatus includes a device for the extraction or separation of reaction products from the burned fuel/oxidant. Especially for the hydrogen chloride synthesis it is provided that the device is designed for a chlorinated compound in the fuel, as well as methane in the oxidant in order to burn the hydrogen chloride and includes a process technological unit after the combustion chamber for extraction of hydrogen chloride or hydrochloric acid. The described arrangement is known to the expert. It is to be remarked, in particular, that the appropriate safety devices are considered and that the materials are accordingly corrosion resistant.
As already discussed, the invention is not only suitable for burning and for hydrogen chloride synthesis, but also as a device for after-burning of waste gases and in this context especially for cleaning. Therefore, problem-free after-burning of components of chlorinated, organic compounds and thereby harmless disposal thereof is possible in some of design examples described below.
Additional measures and characteristic features in the invention result from the following description of one design example, with reference to the enclosed drawing:
Fig. I Partial illustration of a porous reactor line Porous reactor 1 which was previously discussed in more detail was selected for the following design example with which the invention can be implemented and which, in contrast to other reactor types offers special advantages. The essential characteristic of the invention consists in that the flame is cooled through addition of an additional gas to the fuel/oxidant mixture which can be realized in all conceivable reactor types. Therefore, the following description of the design example merely on the bases of porous reactor 1 is not to be regarded as a limitation.
One design foim of an inventive porous reactor 1 is illustrated in Fig. 1. The housing of porous reactor 1 consists of a thin-walled high temperature resistant ceramic interior lining 8, specifically oxide ceramic with a thickness of 2 mm to 50 mm, a graphite support casing 9 and an outside steel casing 10 located at a distance from it. Between the graphite support casing 9 and steel casing 10 cooling water is guided which leaves porous reactor 1 at connection piece 12.
In addition defined zones A ¨ 2, zone B ¨ 4 and zone C ¨ 3 are shown. Zone C ¨
3 is the zone in which burning occurs. Ignition is avoided in zone A -2 by means of appropriate dimensioning.
Zone C- 3 is filled with fillers for this purpose. Zone A -2 in contrast is filled with porous bodies which function as flame arrester. Zone A ¨ 2 and zone c ¨ 3 are distanced from each other by zone B ¨ 4. The wide-coverage temperature monitoring occurs at the interface between zone B ¨
4 and zone C ¨ 3 by means of access of a temperature sensor in the thermometer connecting piece. The gas mixture is led into porous reactor lfrom above, through premixing chamber 5.
The conversion of the reaction mixture occurs in zone C ¨ 3 which is located on support grate 7 and which, in addition is cooled by heat exchanger 11 which is located below it. The wall temperature in reaction zone C ¨ 3 is monitored by wall temperature sensor 13.
Component identification 1 Porous reactor 2 Zone A
3 Zone C
4 Zone B
Premixing chamber 6 Connection piece for temperature sensor 7 Support grate 8 Ceramic interior lining 9 Graphite walls Steel outside walls 11 Heat exchanger 12 Cooling medium connection 13 Wall temperature sensor ILl
Claims (16)
1. Device for burning a fuel/oxidant mixture in an exothermic reaction, said device comprising a reactor with a combustion chamber containing at least one first porous material and at least one second porous material in separate zones, whereby the zones comprise means which enable the exothermic reaction to only occur in the second zone, and with one or more feed lines for the fuel and for the oxidant, wherein zone A
which consists of the first porous material is located at a distance of 10 mm to 4000 mm, equating to one zone B, from zone C which consists of the second porous material and is located vertically before zone C in flow direction of the fuel/oxidant mixture, wherein zone A is located above zone B and C and wherein a support grate is provided at an interface area.
which consists of the first porous material is located at a distance of 10 mm to 4000 mm, equating to one zone B, from zone C which consists of the second porous material and is located vertically before zone C in flow direction of the fuel/oxidant mixture, wherein zone A is located above zone B and C and wherein a support grate is provided at an interface area.
2. Device according to claim 1, wherein the support grate is additionally cooled by a heat exchanger which is located below it.
3. Device according to claim 1 or 2, wherein the distance between zone A
and zone C created by zone B is 20 to 500 mm.
and zone C created by zone B is 20 to 500 mm.
4. Device according to any one of claims 1 to 3, wherein the combustion chamber and the porous material consist of materials which are resistant to temperatures of 1000°C to 2400°C.
5. Device according to claim 4, wherein a temperature monitoring device is located in zone B.
6. Device according to claim 5, wherein an ignition device is located in zone B.
7. Device according to claim 5 or 6, wherein the temperature monitoring device is an infrared sensor.
8. Device according to any one of claims 1 to 7, wherein a premixing chamber is provided for the fuel/oxidant mixture.
9. Device according to claim 8, wherein the premixing chamber comprises means which ensure that the component of the mixture's flow speed in the premixing chamber in relation to the direction of the combustion chamber is greater than the flame speed in the combustion chamber.
10. Device according to claim 8 or 9, wherein a cooling of the premixing chamber is provided.
11. Device according to any one of claims 1 to 10, wherein the porous materials are at least partially in the form of bodies as are used in bulk material of filler bodies or random packing for thermal separation processes.
12. Device according to any one of claims 1 to 11, wherein the combustion chamber comprises means for flame stability during overpressure and/or negative pressure.
13. Device according to any one of claims 1 to 12, wherein combustion chamber temperature equalization is provided for an approximate adiabatic burning control without thermal wall effects.
14. Device according to any one of claims 1 to 13, further comprising an apparatus for extraction or separation of reaction product from the burned fuel/oxidant.
15. Device according to claim 14, wherein it is designed for chlorine or for a chlorinated compound as well as hydrogen or a hydrogenated compound in the fuel/oxidant mixture for extraction of hydrogen chloride through combustion and that it comprises a process technological device for extraction of hydrogen chloride or hydrochloric acid after the combustion chamber.
16
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE102008048359A DE102008048359B4 (en) | 2008-09-22 | 2008-09-22 | Apparatus for combustion of a fuel / oxidizer mixture |
| DE102008048359.1 | 2008-09-22 | ||
| PCT/EP2009/062215 WO2010031869A2 (en) | 2008-09-22 | 2009-09-21 | Device for burning a fuel/oxidant mixture |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CA2738003A1 CA2738003A1 (en) | 2010-03-25 |
| CA2738003C true CA2738003C (en) | 2014-02-11 |
Family
ID=41821055
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA2738003A Expired - Fee Related CA2738003C (en) | 2008-09-22 | 2009-09-21 | Device for burning a fuel/oxidant mixture |
Country Status (8)
| Country | Link |
|---|---|
| US (1) | US8926319B2 (en) |
| EP (1) | EP2347177B1 (en) |
| CN (1) | CN102165256B (en) |
| BR (1) | BRPI0919820B1 (en) |
| CA (1) | CA2738003C (en) |
| DE (1) | DE102008048359B4 (en) |
| RU (1) | RU2487299C2 (en) |
| WO (1) | WO2010031869A2 (en) |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US10281173B2 (en) * | 2012-06-28 | 2019-05-07 | Purpose Co., Ltd. | Burner, combustion apparatus, method for combustion, method for controlling combustion, recording medium, and water heater |
| BR112018005896B1 (en) * | 2015-10-01 | 2022-02-08 | Sgl Carbon Se | COMBUSTION DEVICE FOR THE PRODUCTION OF HYDROGEN HALOGENS |
| CN114183751A (en) * | 2021-11-25 | 2022-03-15 | 北京动力机械研究所 | Closed circulation heat source device based on lithium and sulfur hexafluoride reaction |
Family Cites Families (15)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4392814A (en) * | 1979-06-08 | 1983-07-12 | Can-Eng Holdings Limited | Fluidized bed |
| US4785768A (en) * | 1986-09-15 | 1988-11-22 | Iowa State University Research Foundation, Inc. | Means and method for controlling load turndown in a fluidized bed combustor |
| FR2628511B1 (en) * | 1988-03-10 | 1990-06-22 | Perie Rene | METHOD AND DEVICE FOR COMPLETE COMBUSTION WITHIN A POROUS REFRACTORY BRICK OF A COMBUSTIBLE AND OXIDIZED GAS MIXTURE |
| DE69224239T2 (en) * | 1991-07-05 | 1998-05-20 | Thermatrix Inc | Method and device for controlled reaction in a reaction matrix |
| US5165884A (en) * | 1991-07-05 | 1992-11-24 | Thermatrix, Inc. | Method and apparatus for controlled reaction in a reaction matrix |
| DE4322109C2 (en) | 1993-07-02 | 2001-02-22 | Franz Durst | Burner for a gas / air mixture |
| DE19527583C2 (en) * | 1995-07-28 | 1998-01-29 | Max Rhodius Gmbh | Burners, especially for heating systems |
| NL1005800C2 (en) * | 1996-11-16 | 1999-05-10 | Fasto Nefit Bv | Porous body for gas-burner - has open space at igniter between successive zones |
| DE19939951C2 (en) | 1999-08-23 | 2002-10-24 | Sgl Acotec Gmbh | Method for a burner and a corresponding device |
| DE10228411C1 (en) * | 2002-06-25 | 2003-09-18 | Enginion Ag | Burner for the combustion of a gas/oxygen fuel, has a fine-pore material at the inflow and a coarse-pore material at the outflow, separated to give an intermediate pore-free zone during start-up |
| DE10309799A1 (en) * | 2003-03-05 | 2004-09-23 | Sgl Acotec Gmbh | Method and device for producing hydrogen chloride |
| JP4653082B2 (en) * | 2004-03-30 | 2011-03-16 | 謙治 岡安 | Portable heat transfer device |
| DE502005003727D1 (en) * | 2005-01-31 | 2008-05-29 | Basf Se | Process for the preparation of nanoparticulate solids |
| DE102005044494B3 (en) * | 2005-09-16 | 2007-03-08 | Wenzel, Lothar | Device for removing harmful components from exhaust gases of internal combustion engines |
| AT504398B1 (en) * | 2006-10-24 | 2008-07-15 | Windhager Zentralheizung Techn | PORENBURNER, AND METHOD FOR OPERATING A PORN BURNER |
-
2008
- 2008-09-22 DE DE102008048359A patent/DE102008048359B4/en not_active Expired - Fee Related
-
2009
- 2009-09-21 CN CN200980137226.3A patent/CN102165256B/en active Active
- 2009-09-21 EP EP09744981.3A patent/EP2347177B1/en active Active
- 2009-09-21 CA CA2738003A patent/CA2738003C/en not_active Expired - Fee Related
- 2009-09-21 RU RU2011115810/06A patent/RU2487299C2/en active
- 2009-09-21 WO PCT/EP2009/062215 patent/WO2010031869A2/en active Application Filing
- 2009-09-21 BR BRPI0919820-2A patent/BRPI0919820B1/en active IP Right Grant
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2011
- 2011-03-22 US US13/069,133 patent/US8926319B2/en active Active
Also Published As
| Publication number | Publication date |
|---|---|
| WO2010031869A3 (en) | 2010-07-01 |
| EP2347177B1 (en) | 2018-01-03 |
| CN102165256B (en) | 2015-02-18 |
| RU2011115810A (en) | 2012-10-27 |
| DE102008048359A1 (en) | 2010-04-15 |
| BRPI0919820B1 (en) | 2020-03-24 |
| RU2487299C2 (en) | 2013-07-10 |
| BRPI0919820A2 (en) | 2016-02-10 |
| US20110229835A1 (en) | 2011-09-22 |
| WO2010031869A2 (en) | 2010-03-25 |
| EP2347177A2 (en) | 2011-07-27 |
| DE102008048359B4 (en) | 2010-08-26 |
| CN102165256A (en) | 2011-08-24 |
| US8926319B2 (en) | 2015-01-06 |
| CA2738003A1 (en) | 2010-03-25 |
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